Variable Pulsed Ionic Waste Stream Reclamation System and Method

ABSTRACT

A method for treating wastewater having one or more of suspended solids, dissolved solids, biological oxygen demand includes solids filtration followed by a bi-polar/bi-directional flow through ionic module fitted with anionically/cationically charged plates followed by a sub-sonic resonance module followed by another bi-polar/bi-directional flow through ionic module followed by a ultra-sonic resonance module followed by one or more anion/cation collection membrane modules. Recycle is provided in each step, wherein each step may be repeated, and wherein one or more of the steps can be bypassed.

CROSS-REFERENCE TO RELATED APPLICATIONS

NONE.

STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH

Not applicable.

BACKGROUND

The present invention generally relates to waste stream remediation andmore particularly the use of acoustic energy in combination with ionicenergy and additional unit operations disclosed below.

The initial step in processing a waste stream often begins by taking asample of the given waste stream and subjecting the sample to analysis,which often includes sending it to a certified analytical laboratory todetermine the exact isotopic configuration, or chemical composition,within the given waste stream. The information gathered from thisanalysis is in the form of total suspended solids (TSS), total dissolvedsolids (TDS), biological oxygen demand (BOD), pH, conductivity, andvarious isotopes or elements, as desired by the end user. In addition,particle size distribution (usually in microns) of the total suspendedsolids may be required to determine the level of pre-process filtrationrequired in preparing the waste stream for further processing. The TSSlevel often requires being addressed prior to addressing the TDS andvarious isotopes associated with the TDS. This is not the case for everywaste stream, in that the TSS level may be at a drastically lower ratioto the liquid of the given waste stream.

Typical of prior proposals in this field include, for example:

U.S. Pat. No. 5,549,812 [Witt] discloses enhanced efficiency ofelectrolytic treating industrial wastewater using a specific amount ofhertz in a pulsating direct current supply with sacrificial/consumableelectrodes.

U.S. Pat. No. 5,531,865 [Cole] discloses removing contaminants fromwastewater by passing a stream through an electrolytic oxidation vesselchamber containing anodes in parallel with cathodes.

U.S. Pat. No. 6,887,368 [Khalemsky, et al.] discloses heavy metalselectroextraction from solutions and wastewater by passing the fluidsthrough an electroreactor with two 3-electrode stacks and applying3-phase alternating current to the solution.

U.S. Publication No. 2004/0050781 [Coffey, et al.] discloses waterpurification by electrolytically forming molecular halogen, hypohalicacid and/or hypohalite ions from halide ions dissolved in water anddissolving metal(s) in water to provide metal ion(s), which can besubsequently removed.

U.S. Publication No. 2013/0180857 [Heffernan, et al.] discloses anelectrocoagulation cleaning system for liquid waste into the system witha “heavies” collection unit, electro-coagulation treatment zone andscraping electrode unit.

U.S. Pat. No. 5,792,369 [Johnson] discloses non-chemical plasma ionwater disinfection through a flow control canister.

U.S. Pat. No. 9,096,450 [Andrews, et al.] discloses removing orotherwise reducing the level of contaminants in water.

U.S. Publication No. 016/0031731 [Holland] discloses increasing rate bywhich dissimilar material are separated in water by passing theaqueous-based mixture through an electrically active housing.

Perng, Yuan-Shing, et al.; “Treatment of a specialty paper millwastewater using a pilot-scale pulsed electrocoagulation unit.” Taiwan JFor Sci 3 (2007) discloses purification of an industrial water streamfrom a paper mill using pulsed electrocoagulation with a variety ofelectrode materials.

The disclosed reclamation system will be described in detail below.

BRIEF SUMMARY BRIEF DESCRIPTION OF THE DRAWINGS

For a more complete understanding of the nature and advantages of thepresent method and process, reference should be had to the followingdetailed description taken in connection with the accompanying drawings,in which:

FIG. 1 is a system flow schematic;

FIG. 2 is an isometric view of a bi-polar/bi-directional flow throughionic module;

FIG. 3 is a sectional view taken along line 3-3 of FIG. 2;

FIG. 4 is an isometric view of the module of FIG. 2 with the outer shellremoved;

FIG. 5 is a top view of the anode diffuser ionic electrode plate of thebi-polar/bi-directional flow through ionic module;

FIG. 6 is a top view of the cathode diffuser ionic electrode plate ofthe bi-polar/bi-directional flow through ionic module;

FIG. 7 is a top view of the tri-capacitive ionic diffuser plate of thebi-polar/bi-directional flow through ionic module;

FIG. 8 is an isometric view of the subsonic particle separation module;

FIG. 9 is an end view of the subsonic particle separation module;

FIG. 10 is an isometric view of the ultrasonic particle separationmodule;

FIG. 11 is a bottom view of the ultrasonic particle separation module;

FIG. 12 is an isometric view of the pulsed ionic bi-polar/b-directionalionic membrane collection module;

FIG. 13 is a sectional view taken along line 13-13 of FIG. 12;

FIG. 14 is an isometric view of the pulsed ionic bi-polar/b-directionalionic membrane collection module with the outer shell removed;

FIG. 15 is an end view of an anode diffuser ionic electrode plate of thepulsed ionic bi-polar/b-directional ionic membrane collection module;

FIG. 16 is an end view of a cathode diffuser ionic electrode plate ofthe pulsed ionic bi-polar/b-directional ionic collection module;

FIG. 17 is an end view of the tri-capacitive ionic diffuser plate of thepulsed ionic bi-polar/b-directional ionic collection module;

FIG. 18 is a sectional view taken along line 18-18 of FIG. 13;

FIG. 19 is an isometric view of the membranes stacked on pins for thepulsed ionic bi-polar/b-directional ionic membrane collection module;

FIG. 20 is an electrical schematic of the variable pulse/variablefrequency power supply;

FIG. 21 is the power supply waveform generated by the variablepulse/variable frequency power supply; and

FIG. 22 is a system flow diagram used in the Examples.

The drawings will be described in greater detail below.

DETAILED DESCRIPTION

To better understand the technology disclosed herein, the severalprocess steps performed on any given waste stream are discussedinitially. The initial step in processing a waste stream begins withtaking a sample of the given waste stream to determine the exact contentof the given waste stream. To that end, the sample is analyzed todetermine the exact isotopic configuration, or chemical composition, ofthat given waste stream. An outside laboratory often may perform suchanalysis. The information gathered from this analysis often includestotal suspended solids, (TSS), total dissolved solids, (TDS), biologicaloxygen demand, (BOD), pH, conductivity, and various isotopes orelements, as desired by the end user. In addition, particle sizedistribution, usually in microns, of the total suspended solids isrequired to determine the level of pre-process filtration required inpreparing the waste stream for further processing. For the waste streamtreated herein, the TSS level and various isotopes associated with theTDS should be addressed prior to addressing of the TDS. This is not thecase for every waste stream in that the TSS may be at a drasticallylower ratio to the liquid of the given waste stream.

The treatment scheme disclosed herein will be illustrated by using awaste stream data of an anaerobic digester. The additional isotopicidentification necessary for determining the exact application of thetechnology being presented is as follows: ammonia, nitrate, nitrogen,phosphorous, sulfate, and chloride. Once the above information isobtained, the exact technological application of the disclosed systemcan be implemented in processing the waste stream. It will be understoodthat the disclosed system is sufficiently flexible and powerful to treata wide variety of waste streams containing a multiple of differentcomponents to be removed.

Waste Stream Initial Findings

The waste stream sample data used to illustrate the disclosed system isset forth below:

Total Suspended Solids (TSS) 57,000 PPM (Parts Per Million) TotalDissolved Solids (TDS) 5,700 PPM (Parts Per Million) pH 7.9 (PotentialHydrogen or Alkalinity) Conductivity 26,900 μs/cm (Micro Siemens perCentimeter) BOD (Biological Oxygen Demand) 30,355 PPM (Parts PerMillion) Ammonia Nitrogen 2,657 PPM (Parts Per Million) Chloride 746 PPM(Parts Per Million) Iron 1,853 PPM (Parts Per Million) Calcium Total2,060 PPM (Parts Per Million) Alkalinity Total 13,700 PPM (Parts PerMillion) Nitrate Nitrogen 209 PPM (Parts Per Million) Phosphorous Total1,017 PPM (Parts Per Million) Sulfate 104 PPM (Parts Per Million)Turbidity 43,333 NTU (Nephelometric Turbidity Unit) Waste Stream TotalSuspended 57,000 PPM (100%) Solids (TSS) 100μ (Micron) Particle Size68.4 PPM (0.12%) 70μ (Micron) Particle Size 12,619.8 PPM (22.14%) 50μ(Micron) Particle Size 10,094.7 PPM (17.71%) 20μ (Micron) Particle Size17,208.3 PPM (30.19%) 10μ (Micron) Particle Size 9,137.1 PPM (16.03%) 5μ(Micron) Particle Size 5,848.2 PPM (10.26%) 1μ (Micron) Particle Size1,943.7 PPM (3.41%) 0.01μ (Micron) Particle Size 74.1 PPM (0.13%)

For this waste stream, the TSS was 5.7% of the total volume. Nominalnumbers for any given waste stream typically are 2% (20,000 PPM), orless. For this reason, it was necessary to address the TSS of this wastestream prior to treatment through the system. For some applications, anultra-filter is part of the pre-treatment process in removing organicmatter. By removing organic matter first, the TDS dissociation processhappens at a much more rapid rate which contributes to faster processtimes and lower operating cost.

With this information, it was determined that the waste stream should befiltered down to a 0.01 μ particle size to process the waste streameffectively and efficiently. This is not the case with every wastestream. It must be understood that every waste stream is unique and mustbe addressed individually to determine the best possible application ofany process methodology. As previously stated, TDS levels of 2% or lessusually do not require ultra-filtration, unless these solids are organicmatter, by majority, and the particle size distribution analysisindicates most particles to be less than 1 micron. If this were thecase, the use of an ultra-filter would serve to improve the efficiencyof the system.

Removing Suspended Solids

It must be stated here that not every waste stream requires the level ofpretreatment filtration, as does the waste stream used herein toillustrate the disclosed waste stream schema. Most waste streams canreadily be fed directly into the system for processing. For illustrationpurposes, a disk filtration, micro filtration, and ultra filtration werechosen to implement. This facilitates reducing the particle size to lessthan about 0.01 μ and effectively removes about 99.87% of the totalsuspended solids of this waste stream. Upon completion of the suspendedsolids removal, the sample is now ready to be processed by the disclosedtreatment system.

Chemical Analysis

After the filtration lowering of the TSS, a new chemical analysis of thewaste stream was determined, since the isotope level of components mayhave changed. This is especially true regarding BOD, pH, andconductivity.

The new analysis was obtained from the mass spectrum analysis of thewaste stream to yield a more specific assessment as to the variousisotopic composition of the waste stream. It also provides the amount ofbiological oxygen demand (BOD), turbidity, conductivity, and pH. Forthis test sample, it was determined to concentrate on removal ofammonia, chloride ions, iron, calcium, alkalinity, nitrate, phosphorous,and sulfate.

When analyzing the various isotopes, indication is given that there aremany which lend themselves to molecular bonding with other elementsand/or compounds within the waste stream. Ammonia, when oxidized, willbond readily with chlorides, nitrates, sulfates, and phosphates, thuscreating ammonium chloride, ammonium nitrate, ammonium phosphate, andammonium sulfate. This oxidation/bonding process acts as a contributorin the removal of these compounds in that, as the molecules aredissociated from the water molecule and bond together, they create asolid that can be collected for removal from the waste stream.

Ammonia and Phosphate to Ammonium Phosphate

There is one additional step implemented during the analysis processthat is different from any other known technology. The magneticresonance frequency of a nucleus is determined by the magnetic fieldthat the nucleus is in, and the gyromagnetic ratio of the nucleus. Themagnetic field is referenced in Tesla Units. The standard used toreference this information is a Nuclear Magnetic Resonance PeriodicTable or NMR. In a dry solid form, each of these isotopes would becrystalline in its molecular structure. In a solid form, eachcrystalline structure also would have an acoustic resonance. If thatcrystalline isotope is exposed to a resonant frequency for that givenisotope, a vibration will be induced into the crystalline structure.This vibration, at resonance, will cause friction within the isotope,which in turn causes heat. With the introduction of an electro-magneticfield, the environment is created where a sub-harmonic of the actualnuclear magnetic resonance frequency can be applied to the molecule ofwater and the associated isotope; thus, enhancing the dissociationprocess. This resonant frequency or sub-harmonic resonant frequency isin a range from 20,000 Hz-230,000 Hz. An example, as applied to thiswaste stream, could be explained by using the phosphorous isotope NMRfrequency. According to the NMR Periodic Table, the resonance frequencyfor phosphorous is 202.404 megahertz. There are 4 frequencies within theultra-sonic frequency range of our system that are applicable to thisprocess. There is only one frequency in the sub-sonic frequency range ofthe disclosed system that is applicable. The frequency chosen isdetermined also by the resonant frequencies of the other isotopes withinthe given waste stream. For a given waste stream it is very likely therewill be multiple frequencies used in both the ultra-sonic and sub-sonicranges. The harmonic relationship of the frequencies creates adissonance or disharmony of frequencies induced into the waste stream.This dissonance creates a molecular excitation due to friction createdfrom the dissonant frequencies.

It is the introduction of these dissonant frequencies which, whenintroduced to the water molecule in conjunction with a pulsed electricalsignal of a sub harmonic, causes the water molecule to release itsmolecular bond on the dissolved solids in a process called dissociation.This dissociation of the dissolved solid molecule from the watermolecule, when subjected to the resonant frequency or a sub-harmonicfrequency and the pulsed electrical energy, which is pulsed at asub-harmonic of the resonant frequency, is enhanced even more with theintroduction of a sub-sonic frequency which is the lowest sub-harmonicof the established resonant frequency of a given isotope.

The sub-sonic, pulsed electrical signal, and the ultra-sonic frequenciesare additive when induced simultaneously on the water molecule and,thus, create a greater application of force on the water molecule,causing the water molecule to release or dissociate the dissolved solidback to a semi-solid or solid form.

System Components

The disclosed system consists of several components, as described above,when assembled together, function as a single system to achieve thedesired end results of a clean waste stream. For present purposes, eachcomponent of the system will be disclosed, giving operational parametersas it relates to the previously described waste stream. The exactdetails will be discussed later herein.

-   1. Variable Pulse/Variable Frequency Ionic Generator (Power Supply)    -   a. Operating Input Voltage of 240 VAC    -   b. Output Voltage of 0-24, 0-32, 0-48 Volts Pulsed    -   c. Pulse Rate of 0-600 Hz    -   d. Current of 0-40 Amps    -   e. Waveform: Sine, Square, Saw tooth    -   f. Auto tuning-   2. Bi-Polar/Bi-Directional Flow Through Ionic module (Cell-Ruthenium    Oxide, Iridium Oxide coated, other metal oxide coatings)    -   a. Capacitive Cell    -   b. Tri-Capacitive Cell    -   c. Capacitive Vortex Cell    -   d. Tri-Capacitive Vortex Cell-   3. Subsonic Particle Separation module    -   a. 0-20 Hz (Acoustic Energy-greater than 400 watts per gallon        instantaneous)    -   b. UltraSonic Particle Separation module    -   c. 20 Kilohertz to greater than 230 Kilohertz (Acoustic        Energy-greater than 400 watts per gallon/instantaneous)-   4. Pulsed Ionic Bi-Polar/Bi-Directional Ionic Collection module    (Membrane)    -   a. Cation Module    -   b. Anion Module    -   c. Cation/Anion Module

How it all Works

With the information obtained from the initial laboratory analysis ofthe waste stream, specific operational parameters are programmed intothe system control firmware database network. Once this database hasbeen established, as to the known isotopic composition of the wastestream, the resonant frequency of those isotopes, electricalcharacteristics, and possible isotopic bonding equations, the variablepulse/variable frequency ionic generator (power supply) operationalparameters are established for the bi-polar/bi-directional flow throughionic module and programmed into the system database. These parameterscan include any of the following; frequency, voltage AC and/or DC,current, wave form (sine wave, square wave, or saw tooth wave). Theprocedure is repeated for the variable pulse/variable frequency ionicgenerator (power supply) used to power the anion, cation, andanion/cation pulsed ionic bi-polar/bi-polar directional collectionmodule (pulsed ionic bi-polar/bi-polar directional collection pulsedionic bi-polar/bi-polar directional collection membrane) variations.

The operational parameters of the module then are programmed into thecontrol oscillator. These parameters include frequency, wave shape (sinewave, square wave, saw tooth wave, etc.), and magnitude of the signal.These parameters are established based on the information obtained fromthe waste stream analysis.

The same information is used to establish the operating parameters ofthe ultra-sonic particle separation module. Once the operatingfrequencies have been established, those frequencies are then programmedinto the controller and the UPSM is setup for operation.

Upon completion of the setup of the system control firmware databasenetwork (recipe), the system is then run through an auto tuning processto establish a baseline of operation. This auto tuning process isgenerated from the information stored in the system control firmwaredatabase. The method in which the auto tuning process takes place iscompletely proprietary and part of this patent process. As this baselineis established, the system will auto tune for consistent operationthroughout the given waste stream process procedure.

When the system is turned on and referring to FIG. 1, a waste stream,10, passes through a bi-polar/bi-directional flow through ionic module,12, where the dissociation process begins with ionization of wastestream 10. Module 12 is connected to a power supply, 14. Theintroduction of a pulsed electrical signal will create molecularexcitation of the water molecule. This excitation process also willcreate a friction in the water molecule. The output, 16, from module 14is passed into a sub-sonic resonance module, 18. With the addition ofthe sub-sonic energy in sub-sonic particle separation module 18, boththe electrical pulse and the sub-sonic energy are induced into the watermolecule generating more excitation within the water molecule, promotingthe dissociation process.

Next, the withdrawn waste stream, 20, is passed from module 18 into asecond bi-polar/bi-directional flow through ionic module, 22, where itis once again subjected to another electrical pulse to intensify theionization process. At this point in the discussion, it should bepointed out that the system is fitted with additional piping/valvingsystems to permit the waste stream flow to be recycled through priormodules, bypass certain modules, etc. Such recycle, and bypass lines areshown in the drawings, but will not be discussed herein leaving suchalternative flow patterns to the expertise of the skilled artisan.

After passing through the module 22, a withdrawn waste stream, 24, thenpasses through an ultra-sonic particle separation module, 26, where evenmore energy is introduced to the water molecule, creating even moremolecular excitation and, thus, facilitating the dissociation process.Whether sub-sonic module 18 and ultra-sonic module 26 are separate orhoused within the same chamber is a function of the isotopicconfiguration of the given waste stream. The sub-sonic collection moduleis designed to separate the larger dissociated particles from the watermolecule, while the ultra-sonic collection module is designed toseparate the smallest microscopic particles dissociated from the watermolecule. As each form of energy is imposed upon the waste stream, thewater molecule goes through a process where dissolved solids aredissociated from the water molecule and returned to a semi-solid tosolid state for removal and collection by a pulsed ionicbi-polar/bi-directional collection module (described below). However,before that takes place withdrawn waste stream, 28, is passed through afinal flow through ionizing cell, 30, to impose a strong electricalcharge to create a greater distance between the dissociated solid andthe water molecule. This greater separation is a microscopic coagulationof the dissolved solids in preparation for removal from the waste streamin the pulsed ionic bi-polar/bi-directional collection module. Thiselectrical charge will be beneficial to the removal of the dissociatedisotope in the pulsed ionic bi-polar/bi-directional collection module(membrane). It should be pointed out that, while power supply 14 isshown connected to modules 12, 22, and 26, a separate power supply couldbe connected to each of such modules.

The waste stream is withdrawn from flow through ionizing cell 30 andthen can be passed into any of the banks of modules, as with the overallprocess where streams can be recycled or passed to virtually any of themodules described herein depending upon the waste stream being treatedand the combination of organic and/or inorganic contaminants to beremoved and their concentration. In the system layout of FIG. 1, wastestream 32 will be passed through an anion collection module, a cationcollection module, and finally an anion/cation collection module. Ofcourse, each module could be a series of 2 or more modules with avariety of recycle possibilities as described elsewhere herein. FIG. 1shows a series of 3 of each of the collection modules. Such multiplemodules may be desired to keep the entire system running continuously.That is, each module can be cleaned, maintained, repaired by using oneor more of the other modules, since cleaning involves mere backwashingof each module. If only one module is used, the other 2 modules aremaintained in reserve for adding capacity and/or treatment of the wastestream and/or use when the currently used module needs cleaning,repairing, or maintenance. Of course, the use of 3 of each type ofmodule is for illustration purposes only in that such number could be 1or more. Moreover, the sequence of modules (anionic, cationic,anionic/cationic) could be altered and still be within the disclosureset forth herein.

As ionized waste stream 32 passes through anion collection module, 34,positive charged isotopes, such as nitrates, calcium, magnesium, andsodium, are attracted to and bond to the surface of the membranematerial in anion collection module 34 until the electrical signal isremoved and the membrane is placed in a backwash cycle to flush thedissociated isotopes. As shown in FIG. 1, two anion collection modules,36 and 38, follow module 34, for the purposes described above. Ofcourse, valving appears in each line for additional flow and treatmentpatterns. To that end, valves, 40, 42, 44, and 46, are shown inassociation with the anionic collection modules. Valves 42, 44, and 46permit water to backwash anionic collection modules 34, 36, and 38,respectively. Finally, it should be noted that a power supply, 48, isused to supply the charge to the anionic collection modules.

Upon leaving anion collection module treatment operation, the wastestream then passes through a cation collection module assembly. Negativecharged isotopes, such as, for example, ammonia, phosphate, chloride,and sulfate, are attracted to and bond to the surface of the membranematerial in the cation ion membrane material until the electrical signalis removed and the membrane is placed in a backwash cycle. This alltakes place within the system control firmware database network and iscarried out by the system control program using an Allen Bradley 1768CompactLogix Controller (Rockwell Automation, Milwaukee, Wis.) orequivalent program logic controller (PLC). As shown in FIG. 1, twocation collection modules, 52 and 54, follow cation module 50, for thepurposes described above. Of course, valving appears in each line foradditional flow and treatment patterns. To that end, valves, 56, 58, 60,and 62, are shown in association with the cationic collection modules.Valves 58, 60, and 62 permit water to backwash anionic collectionmodules 50, 52, and 54, respectively. Finally, it should be noted that apower supply, 64, is used to supply the charge to the anionic collectionmodules.

The final module assembly is the anion/cation collection moduleassembly. This module works like the anion and cation module on anypossible molecularly bonded isotopes, such as, for example, ammoniumnitrate, sodium chloride, and potassium sulfate. This module type alsoserves as a second line of defense in collecting any isotope notpreviously collected in either the anion or cation collection modules.Two different sets of such anion/cation collection module assemblies areillustrated in FIG. 1. Of course, depending upon the waste stream beingprocessed, there could be one, two, or more such module assemblies used.

As shown in FIG. 1 for the first such anion/cation module assembly, twoanion/cation collection modules, 68 and 70, follow module 66, for thepurposes described above. Of course, valving appears in each line foradditional flow and treatment patterns. To that end for the firstanion/cation module assembly, valves, 72, 74, 76, and 78, are shown inassociation with the anionic/cationic collection modules. Valves 74, 76,and 78 permit water to backwash anionic collection modules 34, 36, and38, respectively. Finally, it should be noted that a power supply, 80,is used to supply the charge to the anionic collection modules.

As shown in FIG. 1 for the second such anion/cation module assembly, twoanion/cation collection modules, 84 and 86, follow module 82, for thepurposes described above. Of course, valving appears in each line foradditional flow and treatment patterns. To that end for the firstanion/cation module assembly, valves, 88, 90, 92, and 94, are shown inassociation with the anionic/cationic collection modules. Valves 90, 92,and 94 permit water to backwash anionic collection modules 82, 84, and86, respectively. Finally, it should be noted that a power supply, 96,is used to supply the charge to the anionic collection modules.

When the waste stream has passed through the final anion/cationcollection module the waste stream is free of the undesired isotopes.Depending on the end users discharge requirements, the water can bedischarged, reused, or run through a de-ionizing process and finalultrafiltration process prior to discharge to the water-polishingportion of the system. FIG. 1 shows the Clean Water Output dischargedfrom various of the modules in the disclosed system in a line, 98, alongwith a line, 100, for passing the module waste to a backwash dischargetank, 102, where solid waste can be discharged in a line, 104, alongwith a recycle stream, 106, for combining with inlet stream 10 to thesystem.

The amount of water polishing necessary for a given waste stream isdetermined by the level of contaminant removal, as specified by local,state, and federal EPA regulations, the client is required to meet. Thepolishing process is achieved by using accepted standards and practicesfor turbidity, pH, tannin, de-ionization, de-mineralization,de-chlorination, desalination, and others, based on applicable EPAregulations. These discharge levels are part of the system controlfirmware database and are continuously monitored by instrumentationdevices designed to detect such levels. In the event any level isdetected outside the prescribed parameters of operation, as outlined inthe system control firmware database, the system will automatically beswitched to a diagnostic mode which will determine where the parameteris out of operational specifications and takes the necessary steps tocorrect that specific operational parameter, again using the PLCreferred to above. During this time of assessment and correction, anydischarge water will be diverted back upstream where it will bereprocessed for proper discharge levels.

The disclosed system is modular in that the various pieces of equipmentcan be rearranged into a different sequence, each particular module canbe repeated any number of times, different recycle patterns can beimplemented, residence times within each module, and the like, and thesystem still provide for the efficacious treatment of waste streams ofwidely diverse compositions.

Now that the system components and overall schematic of the disclosedwastewater cleaning system have been described, the details of each ofthe system components will be described.

Bi-Polar/Bi-Directional Flow Through Ionic Module

The flow through ionic modules (FTIM) 12 or 14 may be used in 4different configurations. The details of the flow through ionic modulewill refer to module 12 for illustration purposes. While FTIM module 12is shown as circular in cross-section, other cross-sectionalconfigurations may be used. The vortex option is identical in both thecapacitive cell configuration and the tri-capacitive cell configuration,as illustrated in FIGS. 2-7. A diffuser plate, 108, is locatedimmediately adjacent to and inside of an inlet flange, 110. Diffuserplate 108 forces the waste stream to be spread in a manner that causescomplete coverage over the electrode plates for maximum coverage andionization. There are diffuser plates mounted every 12 inches of thelength of the device, such as, diffuser plates, 112 and 114. Eachinterior diffuser plate operates in similar fashion, as does diffuserplate 108 in spreading the waste stream over the entire cross-sectionalarea of module 12. Every other diffuser plate is connected to a powersupply for generating an electrical charge, positive or negative.Diffuser plates 108 and 114 are such electrically energize diffuserplates. Between each electrically charged diffuser plate is anintermediate diffuser plate, such as non-charged diffuser plate 112.

It will be observed in FIG. 3 that every other interior plate extendsthe length of module 12 for their charging with the same charge as theelectrically charged diffuser plates. A plate, 116, is illustrative ofsuch a plate. Interspersed between each longitudinally extending plateis a longitudinally extending plate that is not connected to an externalelectrical charge. A plate, 118, is illustrative of such a non-chargedplate. Again, the longitudinally extending plates are alternated betweenan outside electrically charged collection plate and a non-externallycharged collection plate. It should be apparent that diffuser plates 108and 114, and correspondingly collection plate 116, may be positively ornegatively charged depending upon whether an anionic module, cationicmodule, or anionic/cationic module is desired for the system. In FIG. 4,longitudinally extending collection plates collection plate 114 and 118are seen along with the other longitudinally extending plates, whichwill not be separately numbered so as to not overly confuse thesefigures.

There are directional deflectors mounted on each electrode platesurface, which facilitate a spinning or vortex action of waste stream asit passes through the FTIM. The design aspect of the directionaldeflectors is part of the present disclosure. Deflectors, 120, 122, and124, have been labelled for illustrative purposes. This vortex actionallows for longer exposure to the ionization process before the wastestream leaves the module. This increase in ionization better facilitatesthe dissociation process and cleaning of the given waste stream.

The difference between the capacitive and tri-capacitive cells iselectrical in nature. In the capacitive cell there are two electrodeplates or collector plates, known as the anode and cathode. These platesare connected to the pulse generator output. The cells are bi-polar, andeach electrode plate can be connected to either a positive or negativepotential from the pulse generator. The internal configuration of thecell allows flow to go in either direction; thus, making itbi-directional in flow direction.

The tri-capacitive cell has 2 conductive plates, connected to the outputterminals from the pulse generator, (anode + and cathode −) and 1 set ofcapacitive plates that are inserted between each of the conductiveplates; thus, creating a circuit that electrically looks like 3capacitors connected in series. This cell effectively changes thepolarity of the waste stream as it passes from the positive to negativeor negative to positive plates. This change in polarity of the ionizedmolecule intensifies the amount of molecular excitation of the watermolecule and, thus, generates a greater dissociation effect on the wastestream molecule due to a 180-degree shift in the electro magnetic fieldbeing induced on the water molecule. Of course, the longitudinallyextending electrode collection plates become charged by the chargeddiffuser plates, diffuser plates 108 and 114 in the drawings.

The electrode plates and the capacitive (non-charged) plate are coated,for example, titanium plates. The coating on the titanium plate may beiridium oxide, ruthenium oxide, or a combination of various mixed metaloxides, best designed to treat a given waste stream and beingelectrically stable, resistant to abrasion and repeated electricallycharging. The coating of the titanium prohibits the titanium from beingdeposited in the waste stream as part of the ionizing process, makingthem the most desirable non-sacrificial electrode. If a sacrificialanode or cathode is used in a process, before the waste stream can bedischarged, the metal deposited from the sacrificial anode or cathodemust be removed from the waste stream.

In addition, each electrode plate and capacitive plate are designed alsoto operate as a diffuser to facilitate maximum coverage and exposure ofthe waste stream to the electrode array.

Sub-Sonic Particle Separation Module

The next component in the system is the sub-sonic particle separationmodule identified as module 18 in FIG. 1. The purpose of this module isto induce a sub-harmonic frequency to the NMR resonant frequency of theidentified isotopes within the waste stream. This sub-harmonic frequencyis in the sub-sonic frequency range of 0-20 Hertz. This sub-sonicfrequency can be a sine wave, square wave, or sawtooth waveform,depending on the intensity of the signal required to dissociate theheavy particles from the waste stream. Sub-sonic particle separationmodule 18 is mounted between 2 of the flow through ionizing modules. Theenergy of the sub-sonic frequency being induced into the waste stream isbetween about 25 watts and 10,000 watts per gallon, instantaneously. Theminimum amount of energy required to impact the dissociation process ofa molecule of water, whether electrical or acoustical, is 25 watts pergallon. The energy imposed on the water molecule creates friction, whichcreates a molecular excitation and better enhances the dissociationprocess of the isotope from the water molecule. While module 18 is shownin rectangular cross-section in FIGS. 8 and 9, circular, hexagonal, orany other geometrical cross-section may be used. The waste streamtreated on module 18 is withdrawn through an outlet, 126, located in atop cover, 128. The inlet and bottom cover plate are not visible in thedrawings.

Ultra-Sonic Particle Separation Module

Working in conjunction with the sub-sonic particle separation module isultra-sonic particle separation module 26. This module also is placedbetween 2 of the flow through ionizing modules. Like sub-sonic module18, the energy from the ultra-sonic frequency being introduced into thewaste stream is between about 25 watts and 10,000 watts per gallon,instantaneously. The added effect the ultra-sonic energy, electricalpulse and the sub-sonic energy, impact on the water molecule, creatingthe dissociation process, which causes the dissolved solid isotope isreleased back to a semi-solid to solid state where it can be removedfrom the waste stream by the pulsed ionic bi-polar/bi-polar directionalcollection modules. The operational range of the ultra-sonic particleseparation module is between 20,000 and 230,000 hertz. The finalfrequency is based upon the isotopic analysis of the given waste streamand the understanding of the resonant frequency of the various isotopeswithin the waste stream and is a sub-harmonic frequency of the NMRresonant frequency of a given Isotope. While module 126 is shown inrectangular cross-section in FIGS. 10 and 11, circular, hexagonal, orany other geometrical cross-section may be used. The waste streamtreated on module 126 is withdrawn through an outlet, 130, located in atop cover, 132, which also is fitted with ultrasonic horns. The inletand bottom cover plate are not visible in the drawings.

Pulsed Ionic Bi-Polar/Bi-Polar Directional Collection Module (Membrane)

The final component in the system is the pulsed ionic bi-polar andbi-directional collection modules or membrane identified as modules 66,68, 70, 82, 84, and 86 in FIG. 1. These modules may be configured in oneof three variations: the anion or negative, the cation or positive, andanion/cation or positive/negative. The membrane material used inmanufacturing these devices is a woven matrix, ion exchange polymer,configured in either as a strong base or strong acid, such as AMI-7001anion exchange membranes and CMI-7000 cation exchange membranesavailable from Astom Corporation (Tokyo, Japan). Of course, othercommercially available similar charged membranes may be used.

The anion modules are designed with an encapsulating ion electrode arraysurrounding the anion membrane particle separation material. Because theanion membrane material is of a negative charge, the positive electrodeis designed to be immediately adjacent to the membrane material in thismodule; thus, pushing the dissociated charged particle away from theelectrode and toward the membrane material. The membrane material alsois configured inside the electrode array whereby the axial positioningof the material is rotated 90 degrees every six inches of linear length.This creates a laminar flow within the module and contributes toconsistent flow and pressure in the module. It also prohibits themembrane material from channeling and, thus, creates a maximum exposureof the waste stream to the membrane material. The purpose of themembrane material is to attract and capture the ionically charged anionisotopes dissociated from the waste stream.

In FIGS. 13 and 18, a positively charged plate, 134, is adjacent to anend plate, 136, having a waste stream inlet, 138, penetratingtherethrough for inlet flow of the waste stream into module 66, whichwill used illustratively herein. On the outlet side, a positivelycharged plate, 140, is adjacent to an end plate, 142, having a wastestream outlet, 144, penetrating therethrough for outlet flow of thewaste stream from module 66. Disposed intermediately is an intermediateflange, 146, which is not connected to an external electrical source.The design in the drawings calls for 12 inches distance betweenintermediate flange 146 and each end plate 134/140. The membrane stacksare rotated 90° every 6 inches along the lengthwise extent of module 66;thus, causing the flow to change directions for minimizing flowchanneling. Each membrane stack is composed of 330 layers of chargedmembrane in the illustrated design. The design encourages the wastestream to flow in relatively thin film flow uniformly along thecross-section of module 66.

Disposed around the membrane stacks are longitudinally extendingelectrodes carrying either an anionic, cationic, or alternatinganionic/cationic charge depending upon the charge impressed on theflange plates connected to the power supply for each module—power supply80 for module 66 described herein. Such electrodes are charged theopposite of the membrane charge, as described above. In FIG. 18,electrode sets, 148, 150, 152, and 154, surround a membrane stack, 156.In FIG. 19, a membrane stack, 157, is carried by pins, 153 a-153 d.

The cation module is physically designed like the anion module with oneexception. In the cation module, the negative electrode is designed tobe immediately adjacent to the membrane material. The configuration ofthe membrane material is identical in all three configurations of thisdevice. The other physical characteristics of the module are identicalto the anion module. The purpose of the cation material is to capturethe ionically charged cation isotopes dissociated from the waste stream.

The anion/cation module is just as the name describes. It is acombination of both materials configured in a layered fashion,alternating between negative and positive on each layer. As with theanion and cation modules, the corresponding electrode is locatedadjacent to a like polarity membrane material. In addition, thismaterial is rotated axially 90 degrees, every 6 inches of lineardistance. The purpose of the anion/cation module is to attract andcapture those combined and/or remaining isotopes.

As with the flow through ionizing cell, each electrode plate also servesas a diffuser to facilitate maximum coverage and exposure of the wastestream to the membrane material.

Variable Pulse/Variable Frequency Ionic Generator (Power Supply)

The VPFIG illustrated in FIG. 20 has multiple functions within theoverall operation of the system. It serves to provide the pulsed energyto two devices, the bi-polar/bi-directional flow through ionic moduleand the bi-polar/bi-directional pulsed ionic particle collection module.Outside of this application, this device can operate as a variable speedmotor controller, an AC power supply with multiple waveform outputs, ora pulsed DC power supply. With the addition of filter capacitors acrossthe output terminals, the DC supply would not be pulsed. In addition,with the addition of regulating diodes, the power supply could bedescribed as a regulated power supply.

Research has shown a pure DC or AC voltage and current, alone, will notcreate the necessary molecular excitation required to cause adissociation process to occur within the given waste stream,economically and efficiently. In this application other manufacturersoperate at 12,000 watts per device. The disclosed system operates at 960watts per device, which is 92% less than other manufacturers. The VPFIGis designed to provide a variable frequency, variable voltage, variablecurrent, variable waveform, AC or DC voltage, and AC and DC voltagesimultaneously, which generates a molecular excitation within the watermolecule; thus, facilitating the dissociation process. For the wastestream we are using herein, the the VPFIG is designed to operate at 0-24volts, 0-40 amps, pulsed at 120 Hz, as can be seen in FIG. 20.

In particular, 240 VAC is passed via lines L1 and L2 into the powersupply through a pair of switches, 158 and 160, respectively. When theseswitches are in the down position, power is passed via lines, 162 and164, into a frequency controller, 166. A pair of output switches, 168and 170, in output lines, 173 and 175, pass power to a pair of 3-wayswitches, 176 and 178, respectively. These 3-way switches can be set topass the frequency control signals to one of the cells described inconnection with FIG. 1.

Alternatively, switches 158 and 160 can pass the input line power passan inductor, 163, connected in turn to a transformer, 164. Note that alight bulb, 166, runs between the two input lines for a visual cue thatpower is present in this circuit. Power from transformer 164 then passesthrough a pair of switches, 169 and 171, which can be positioned to passthe power into a diode bridge, 172, for generation of a pulsed signal.The positive and negative outputs from diode bridge 172 are connectedvia a pair of lines, 174 and 177, to 3-way switches 176 and 178. In theother position, switches 169 and 171 can per the power to be passeddirectly via lines, 180 and 182, respectively, to 3-way switches 176 and178 bypassing diode bridge 172. Finally, FIG. 21 shows the waveformsgenerated by the disclosed power supply at 24 V at two differentfrequencies, as labeled thereon.

While the apparatus, system, and method have been described withreference to various embodiments, those skilled in the art willunderstand that various changes may be made, and equivalents may besubstituted for elements thereof without departing from the scope andessence of the disclosure. In addition, many modifications may be madeto adapt a situation or material in accordance with the teachings of thedisclosure without departing from the essential scope thereof.Therefore, it is intended that the disclosure not be limited to theembodiments disclosed, but that the disclosure will include allembodiments falling within the scope of the appended claims. In thisapplication all units are in the metric system and all amounts andpercentages are by weight, unless otherwise expressly indicated. Also,all citations referred herein are expressly incorporated herein byreference.

The following example shows how the disclosed wastewater treatmentsystem has been practiced. This example is given for illustrationpurposes and should not be interpreted as a limitation on the instantdisclosure.

EXAMPLES Example 1

The process equipment and configuration used in this example is setforth in FIG. 22. Basically, the wastewater flowed from a tank, 184,through a sediment filter, 186, a GAC filter, 188, anion filter, 190,and into a flow through ionic cell, 192. From FTIC 192, the wastewatercould be recycled into tank 184 for additional treatment, or passed intoa sub-sonic treatment tank, 194. Again, the wastewater from sub-sonictreatment tank 194, then was passed through a sediment filter, 196, aGAC filter, 198, cation filter, 200, and back into sub-sonic treatmenttank 194. Again, this loop could be repeated. Alternatively, thewastewater was passed from sub-sonic treatment tank 194 into asuper-sonic treatment tank, 204. From there, again the wastewater waspassed through a sediment filter, 206, a GAC filter, 208, anion/cationfilter, 210, and back into super-sonic treatment tank 204.

To a 70° lot of 100 gallons of municipal water with a projected totaldissolved solids (TDS) of 60 parts per million (ppm) was added 60 poundsof calcium chloride and 20 pounds of sodium chloride. The actual TDSlevel as determined by an independent laboratory was 72,000 ppm. Theobjective of this test was to simulate removing dissolved solids from awaste stream typically found in a natural gas refinery. These dissolvedsolids are in the form of the added salts.

A one-inch diameter airline was placed in the waste tank of the saltsolution and 100 psi of air pressure applied. This caused a vigorousmixing of the water and salts, facilitating the dissolving of the saltsinto solution. After a period of several hours of this mixing process,it was determined the salts to be fully dissolved into solution.

A sample of the water was collected and sealed according to laboratorystandards and marked with date, time, and temperature, and then setaside for the independent laboratory to evaluate.

The initial step to remove the dissolved solids from the wastewatersolution was the ionization and filtration process. The first step ofthis process is to recirculate this waste stream through flow throughionic cells, which were powered by a pulsed ionic generator. The settingfor this pulsed ionic generator was 0-21.8 volts pulsed at 120 Hz, setto a current output of 0-40 amps. This ionization process is thebeginning of the dissociation process to remove organic matter anddissolved solids from the water molecule. If this ionization processwere to take place in a steady state tank, a green organic materialwould be seen coagulating in the body of water. Since we arerecirculating the waste stream, the microscopic organic matter does nothave time to coagulate or collect in a manner that is visible.

As the waste stream goes through a pulsed ionization process, it also isfiltered before re-entering the storage tank. There are multiple filtersconfigured to facilitate the removal of the organic matter and thevarious dissolved solids that have been dissociated from the watermolecule. The first filter was an inline 1-micron sediment filter. Thisfilter can be as small as 0.01-microns on down to the ultrafiltrationrange. For the purposes of this test, a 1-micron filter was selected.After the 1-micron sediment filter, the waste stream was passed througha granulated activated charcoal or GAC filter. During the ionizationprocess, the salts begin to dissociate from the water molecule in theirbasic elemental form. For this waste stream, the basic elements arecalcium, sodium, and chloride ions.

The pulsed ionization process induces a pulsed electrical current intothe water molecule. This pulsed electrical current causes the watermolecule to lose the covalent bond it has on the dissolved ions. Theprocess of breaking this covalent bond is called dissociation. Researchhas shown that by removing the organic matter first, the basic elements,which have been dissolved into solution can be more readily dissociated.

As the pulsed ionization process induces the pulsed electrical currentinto the water molecule the dissociation process begins to take place.As the chloride is dissociated from the water molecule it is convertedfrom a chloride ion to chlorine. The chlorine is a negatively chargedparticle. The GAC filter is designed to attract the chlorine molecule asit is passed through the GAC filter media because it is charged to apositive potential, which causes the attraction of the chlorinemolecule. This attraction process removes the chlorine from the watermolecule.

This completes the first step of the cleaning process. With the organicmatter out of the way for of the chlorides, calcium, and sodium out ofthe way, we transfer the waste stream to a second process tank. In thisprocess tank we repeat the pulsed ionization process and introduceanother for of energy. This form of energy is sub-sonic sound waves oracoustical energy. The frequency introduced is derived from informationobtained from a Nuclear Magnetic Resonance Periodic Table, (NMR). Theinformation from the NMR gives us the specific resonant frequency of agiven Isotope, such as chloride, calcium, and sodium. The sub-sonicfrequency we select is in a range of 0-20 Hertz and is below the rangeof human hearing. The selected frequency is a sub-harmonic frequency ofthe resonant frequency information obtained from the NMR. The selectionof the 120 hertz pulsed electrical energy is also a sub-harmonicfrequency of the resonant frequency. These two types of energy areadditive when imposed simultaneously upon the water molecule.

Because not all the chlorides, calcium, and sodium were removed in theinitial pulsed ionization process, it is necessary to repeat the processin introduce this second form of energy. The long wavelength of thesub-sonic frequency and the pulsed ionic electrical current together,cause the larger particles to dissociate from the water molecule, wherethey are filtered out using the same filtration process in the previoussteps.

As the sub-sonic with pulsed ionization steps and filtration iscompleted, the waste stream is transferred to the next tank. During thisstep we are concentrating on the smallest particles still bonded to thewater molecule. During this step we continue the pulsed ionizationprocess and introduce a third form of energy. This form of energy isultra-sonic energy. This too is another form of acoustical energy abovethe range of human hearing. The range of the frequencies used in thisprocess was from 20,000 hertz to 230,000 hertz. The wavelength of thesefrequencies is extremely short and designed to attack the smallest ofmicroscopic particles, which have maintained their covalent bond to thewater molecule. The selected in the ultra-sonic range is also asub-harmonic frequency obtained from the information on the NMR,regarding the associated Isotopes of the waste stream.

During the third stage of the process, the pulsed ionic current and theultra-sonic sound waved are imposed on the water moleculesimultaneously. The magnitude of energy now being imposed on the watermolecule causes a break in the remaining covalent bond maintainedbetween the water molecule and any remaining chloride, calcium, andsodium ions. As this covalent bond is broken the electrical charge takenon by the given ion facilitate removal from the waste stream in thefinal filtration process.

The final filtration process consists of three filters. The first filteris a 0.01-micron ultra-filter, which is designed to remove the smallestparticles dissociated from the water molecule. The second filter is GAC.This is designed to facilitate the removal of any additionallydissociated chlorine or chloride molecules. The third stage offiltration is now a mixed bed filter of both anion and cation media. Theanion media will attract any of the remaining calcium and sodium. Thecation media will attract any of the remaining chloride or chlorine, notremoved in the GAC filter.

Because the system configuration used for this test was not designed tofacilitate a backwash process for the various filters, each filter wasremoved allowed to open air dry. The collected material in each filterwas reflective of the design specifications of each filtration process.The sediment filter contained a green organic matter, resembling greenalgae. The GAC filter had crystalline structures resembling theappearance and smell of chlorine crystals. The anion and mixed filtermedia had crystalline structures resembling and smelling like calciumand sodium. To prove the collection of sodium, small portions of the drypowder were collected and subjected to destruction testing with a hammeron a hard surface. The dry powder reacted much like pure dry sodiumwould react and gave a sound like a child's toy cap gun.

After the waste stream was passed through the final stage of filtration,a second sample was taken, and measurement logged. The initial resultswere a pH of 7.8, TDS level of 23, and temperature of 78° F. Theindependent laboratory findings are contained in the report dated Dec.20, 2016. The lab report results indicated the starting TDS level was72,000 PPM and the ending TDS level was 20 PPM.

Example 2

This test was an actual test of the waste stream from a plant located inWyoming. For this test, 50 gallons of the actual waste stream from theWyoming LTG refinery was used. Prior to testing a sample was collectedand labeled for processing by an independent laboratory.

The processing was the same as reported in Example 1 using the processconfiguration described in connection with FIG. 22. This waste streamhad a pH of 12, TDS of 59,000, and temperature of 78° F.

The findings of the independent laboratory were as follows: initial TDS55,700 mg/L (dry) and pH 12.2. Post processing, the TDS was 17.0. Forthis test pH was not reported by the lab.

Example 3

275 gallons from an anaerobic digester waste from a commercial plantlocated in Wisconsin with total suspended solids of 57,000 ppm wassubjected to the same process configuration as described above inconnection with FIG. 22 and as used in the prior examples.

Due to the viscous nature of the anaerobic digester waste stream, acomplete network of pre-process filtration was required to remove thelarge volume of total suspended solids from the waste stream. The firststage of this filtration process was accomplished using steel meshscreens. This was done manually by pouring the waste stream through themesh screens, removing the largest clumps of waste material. Thisprocess was repeated until there were no longer any visible clumps ofmaterial.

Upon completion of the rough filtration, the waste stream was filteredagain through a cloth filter, which would pass particles larger than 150microns. When this was completed, the waste stream could then be pumpedthrough incrementally smaller micron filters until we had process thewaste stream down to 1 micron.

After reducing the particle size to 1 micron, the waste stream then waspassed through an ultra-filter, reducing the particle size down to 0.01microns. At this point the waste stream became an amber or gold color,much like gasoline.

Observations were notated as to color, smell, pH, and TDS. The liquidwas now clear, but still a golden color. The pH had been reduced to 7.5while the TDS and TSS were reduced to less than 1,000 PPM. The smell wasno longer a strong ammonia smell, but a milder ammonia odor whichrevealed the stronger sulfur and animal waste smell.

The operational sequence of our laboratory system had not been changedsince the previous tests were completed. The purpose for this non-changewas to prove that the disclosed process could treat a totally unknownwaste stream to satisfactory EPA standards for discharge. Thisnon-change also demonstrated a non-chemical treatment to the wastestream as part of the cleaning process. This was done for demonstrationpurposes, as this waste stream contained live bacteria cultures and itis desired that a commercial system be able to recover these bacteriafor reuse in the anaerobic digester process.

It must be stated at this point that had the independent laboratoryanalysis been available, the system would have been configured slightlydifferently for this test. Nevertheless, the ability and flexibility ofthe basic process is demonstrated in this example.

When the initial filtration process was completed, the anaerobicdigester waste stream was pumped through the flow through ionic cellwhere it is introduced to the pulsed ionic current induced through theionic cells from the pulsed ionic generator. As the material is pumpedthrough the ionic cell, there are several things that take place duringthis part of the cleaning process. The first thing that happens is theionization of the water molecule begins to occur. This ionization is aresult of the pulsed ionic current being applied to the flow throughcell electrode plates from the pulsed ionic generator, charging thewater molecule. In addition, this electrical charge causes molecularexcitation within the water molecule and the ionic dissociation processbegins to take place. This dissociation process is where the dissolvedsolids within the water molecule are released from their covalent bondwith the water molecule and dissociated from the water molecule.

As the isotope is dissociated from the water molecule, an electricalcharge is induced into the isotope. There is one other thing that beginsto take place in this waste stream that must be notated here. This wastestream contains several isotopes that lend themselves to a molecularbond with each other. They are ammonia, nitrates, phosphorus, andsulfate.

As each of these isotopes begins to take on an electrical charge, anddue to the amount of electrical current being pulsed through the wastestream, an oxidation process begins to occur within the variousisotopes. An example of this is ammonia begins to change to an ammoniumion. As it changes states, it becomes able to create a molecular bondingwith the other isotopes; thus, creating, for example, ammonium nitrate,ammonium phosphate, ammonium sulfate. These components are recoverablefor use in other applications.

After processing the waste stream through the flow through ionizingcell, the waste stream was pumped through the first stage of filtration,Zeolite. The function of Zeolite is to remove any ionized ammoniamolecules from the waste stream.

The waste stream then was processed through another stage of the flowthrough ionic cell. This additional ionic charge facilitated the removalof the other dissociated isotopes in the flow through ionic membranes.After process through the flow through cell, the waste stream was passedthrough 3 stages of pulsed ionic membrane material. At this point thecolor of the waste stream had changed even more. It must be notated theTDS level of the waste stream had been reduced from 57,000 PPM down to146.4 PPM.

The next part of the process was to treat the color of the waste streamfor turbidity or color. The waste stream was passed through a turbidityfilter. After passing through a turbidity filter, the waste stream waspassed through granulated activated charcoal and a final filtration forpH balance. This final stage of pH balance introduced some calcium andmagnesium minerals back into the waste stream, raising the final TDSreadings to 364 PPM.

In summary, as stated earlier herein, the laboratory systemconfiguration was non-changed for the processing of this waste stream.Also, previously stated was the fact the ammonia was removed from thewaste stream immediately after the first stage of pulsed ionization. Ina commercial unit, the ionization process would be conducted for a muchlonger period, allowing for a covalent or molecular bonding to takeplace between the various isotopes within the waste stream, as describedearlier herein. In addition, there was no chemical treatment added tothis test. In a commercial unit, due to the high level of bacteriaculture present, a chlorine chemical treatment would be added prior tothe ionization process. This chloride treatment would kill any remainingbacteria in the waste stream and facilitate the system's ability toprocess the waste stream to clean drinking water standards, thusdemonstrating the full capability of the system.

The independent laboratory findings for the initial waste stream and thefinal cleaned waste stream are set forth below.

Measurement Initial Final TDS 5,700 mg/L 364 mg/L Ammonia 2,657 mg/L 2.5mg/L Calcium 2,060 mg/L 20 mg/L BOD 30,355 mg/L 15 mg/L Nitrogen <2 mg/L<0.10 mg/L Phosphorus 1,017 mg/L 1.1 mg/L Sodium 1,245 mg/L 7.0 mg/LSulfate 104 mg/L 1.2 mg/L Turbidity 43,333 NTU 6.8 NTU Conductivity26,900 um/cm 392 um/cm Iron 1,853 0.05 mg/L

1-5. (canceled)
 6. A bi-polar/bi-directional flow through ionic module,which comprises: (a) housing having an inlet and an outlet, wherein theinlet is fitted with a diffuser plate; (b) longitudinally extendingelectrically charged longitudinally extending collection plates disposedwithin the housing; and (c) non-electrically charged plates interposedbetween the electrically charged longitudinally extending collectionplates.
 7. The bi-polar/bi-directional flow through ionic module ofclaim 6, wherein the collection plates are fitted with vortex plates. 8.The bi-polar/bi-directional flow through ionic module of claim 6,wherein sets of the longitudinally extending electrically chargedlongitudinally extending collection plates are rotated 90° from eachother.
 9. The bi-polar/bi-directional flow through ionic module of claim6, wherein the collection plates are coated with a metal oxide. 10-19.(canceled)